CN110252216A - A kind of fluidized-bed reactor taking heat for methane conversion and intensification - Google Patents
A kind of fluidized-bed reactor taking heat for methane conversion and intensification Download PDFInfo
- Publication number
- CN110252216A CN110252216A CN201910331433.8A CN201910331433A CN110252216A CN 110252216 A CN110252216 A CN 110252216A CN 201910331433 A CN201910331433 A CN 201910331433A CN 110252216 A CN110252216 A CN 110252216A
- Authority
- CN
- China
- Prior art keywords
- fluidized bed
- fluidized
- bed
- heat exchanger
- air inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
- C07C2/82—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling
- C07C2/84—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling catalytic
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
Abstract
The present invention relates to a kind of fluidized-bed reactors that heat is taken for methane conversion and intensification, a kind of fluidized-bed reactor taking heat for methane conversion and intensification, the fluidized bed of ethylene processed is converted including two methane, one heat exchanger of each fluidized bed gas outlet connection, the first fluidized bed (1) bottom end is equipped with the first primary air inlet (1a) and the first extra-air inlet (1b), first primary air inlet (1a) is entered in the first fluidized bed (1) reaction chamber by the first distribution grid (1j), first extra-air inlet (1b) is entered in the first fluidized bed (1) reaction chamber by the first distributor pipe (1g).
Description
Technical field
The present invention relates to a kind of fluidized-bed reactors that heat is taken for methane conversion and intensification, in particular to methane one-step method system
Ethylene strengthens the fluidized bed for taking heat.
Background technique
Ethylene is petrochemical industry and the staple product of organic chemical industry, and with the development of world economy, the demand of ethylene will
Increase year by year, raw material more lighting and cleans.Catalyst for Oxidative Coupling of Methane (OCM) is the important skill for producing ethylene technology
Art, ethylene can be obtained through one step of oxidative coupling under the action of catalyst using natural gas as raw material in it, with low energy consumption, process
Simple advantage.
In recent years, both at home and abroad some researchers OCM Catalyst Conversion, selectivity and in terms of done it is big
The improvement of amount improves the yield of ethylene.Wherein, using Siluria company, the U.S. as representative, the OCM of exploitation is urged for foreign countries
Agent has entered the pilot scale stage in fixed bed reactors；Domestic Chinese Academy of Sciences Lanzhou Chemical Physics research institute is directed to OCM process, opens
Na is sent out2WO3-Mn/SiO2Catalyst has a good application prospect.It is worth noting that Chinese Academy of Sciences's Dalian Chemical Physics research
The anaerobic catalyzed conversion technique for producing ethylene developed, obtains extensive concern both domestic and external.
The research and development of effective catalyst advance the process of industrialization of OCM technology, but OCM process is strongly exothermic, Temperature Distribution not
The features such as, reduces the service life of catalyst.Therefore, it is extremely urgent to develop a kind of OCM reactor for efficiently taking heat.Currently used for
The type of reactor of OCM reaction process mainly has fixed bed reactors and fluidized-bed reactor, and fluidized-bed reactor has temperature
Uniformly, efficiently take heat, can online more catalyst changeout, easily enlargement production the advantages that, become the emphasis of technical research.
Summary of the invention
The present invention converts the response characteristic of ethylene processed for methane oxidation coupling, provide it is a kind of have methane high conversion,
Ethylene is highly selective and the methane conversion and intensification of high yield takes the fluidized-bed reactor and technique of heat.
It is as follows using technical solution in order to reach the purpose of the present invention:
A kind of fluidized-bed reactor taking heat for methane conversion and intensification, the fluidized bed of ethylene processed is converted including two methane, often
One heat exchanger of a fluidized bed gas outlet connection, the first fluidized bed (1) bottom end are equipped with the first primary air inlet (1a) and the first pair
Air inlet (1b), the first primary air inlet (1a) are entered in the first fluidized bed (1) reaction chamber by the first distribution grid (1j), and first is secondary
Air inlet (1b) is entered in the first fluidized bed (1) reaction chamber by the first distributor pipe (1g), and the first fluidized bed (1) reacts cavity outer wall
It is made of the first refractory material (1h), has the first heat exchanger tube (1f) on the first fluidized bed (1) reaction cavity wall, in the first heat exchanger tube
There is the first cooling medium inlet (1d) below (1f), there is the first cooling medium to export (1e) above the first heat exchanger tube (1f), the
One fluidized bed (1) top is equipped with first gas outlet (1c), and second fluidized bed (2) is identical as the first fluidized bed (1) structure.
The first raw material reaction gas (5b) passes through the first distribution from the first primary air inlet (1a) of the first fluidized bed (1)
Plate (1j) enters in the first fluidized bed (1) reaction chamber, and the second raw material reaction gas (5a) is divided into two-way, all the way from the first fluidized bed
(1) the first extra-air inlet (1b) is entered in the first fluidized bed (1) reaction chamber by the first distributor pipe (1g), all the way from second
The second extra-air inlet (2b) for changing bed (2) is entered in second fluidized bed (2) reaction chamber by the second distributor pipe (2g), first class
Bed (1) product gas exports (1c) from first gas, and the of second fluidized bed (2) is entered after cooling down by First Heat Exchanger (3)
Two primary air inlets (2a) are then entered in second fluidized bed (2) reaction chamber by the second distribution grid (2j), second fluidized bed (2)
Product gas from second gas outlet (2c) discharge, by the second heat exchanger (4) it is cooling after be discharged, the first low-temperature cooling media
(6a) divides two-way respectively from the second of the first low-temperature cooling media import (1d) of the first fluidized bed (1) and second fluidized bed (2)
Cooling medium inlet (2d) enters the first heat exchanger tube (1f) and the second heat exchanger tube (2f), and the first High-temperature cooling after heating is situated between
Matter (7a) is exported from the second cooling medium of the first cooling medium of the first fluidized bed (1) outlet (1e) and second fluidized bed (2)
(2e) outflow, the second low-temperature cooling media (6b) divide that two-way respectively enters First Heat Exchanger (3) and the second heat exchanger (4) is changed
Become the outflow of the second High-temperature cooling medium (7b) after heat.
First distribution grid (1j) and the second distribution grid (2j) is sintered plate or porous plate.
First distributor pipe (1g) and the second distributor pipe (2g) is sintering tube or antipriming pipe.
The height of first distributor pipe (1g) and the second distributor pipe (2g) lower than the first cooling medium outlet (1e) and
Second cooling medium exports (2e).
The first raw material reaction gas (5b) is the mixed gas of methane or methane and oxygen；Second raw material reaction gas
(5a) nitrogen or nitrogen and oxygen mixed gas.
The cooling medium (the first low and high temperature cooling medium is identical with the second low, high cooling medium) is water, water steaming
Vapour or water and steam mixture.
The thermal insulation material (the first thermal insulation material and the second thermal insulation material) is alumina silicate and aluminium oxide.
The present invention has the advantages that
1, catalyst is in fluidized state in fluidized bed, is conducive to mass-and heat-transfer, guarantees that temperature is uniform in fluidized bed, avoids
Hot-spot.
2, unstripped gas classification enters fluidized-bed reactor, increases fluidized bed runing adjustment means, ensure that fluidized bed is grasped
The security and stability of work.
3, the methane/oxygen ratio of fluidized bed is adjustable, realizes the high conversion of raw material methane and the height of product ethylene
Selectivity.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of fluidized-bed reactor of the present invention and technique；
In figure: 1, the first fluidized bed, 2, second fluidized bed, 1a, the first primary air inlet, 2a, the second primary air inlet, 1b, the first pair
Air inlet, 2b, the second extra-air inlet, 1c, first gas outlet, 2c, second gas outlet, 1d, the first cooling medium inlet,
2d, the second cooling medium inlet, 1e, the first cooling medium inlet, 2e, the second cooling medium inlet, 1f, the first heat exchanger tube, 2f,
Second heat exchanger tube, 1g, the first distributor pipe, 2g, the second distributor pipe, 1h, the first refractory material, 2h, the second refractory material, 1j,
One distribution grid, 2j, the second distribution grid；3, First Heat Exchanger, the 4, second heat exchanger, 5a, the second raw material reaction gas, 5b, the first original
Expect reaction gas, 6a, the first low-temperature cooling media, 6b, the second low-temperature cooling media, 7a, the first High-temperature cooling medium, 7b, second
High-temperature cooling medium；8 be product gas.
Specific embodiment
Embodiment 1
A kind of fluidized-bed reactor taking heat for methane conversion and intensification, the stream of ethylene processed is converted including two methane oxidation couplings
Change bed, each fluidized bed gas outlet is connected with heat exchanger, the first fluidized bed 1, First Heat Exchanger 3, second fluidized bed 2, second
Heat exchanger 4 is sequentially connected in series.1 bottom end of the first fluidized bed is equipped with the first primary air inlet 1a and the first extra-air inlet 1b, and first is main
Air inlet 1a is communicated with the first distribution grid 1j, and the first extra-air inlet 1b is communicated with the first distributor pipe 1g, in the first fluidized bed 1 under
Portion is built-in with the first heat exchanger tube 1f, the first heat exchanger tube 1f in the first refractory material 1h, has first below the first heat exchanger tube 1f
Cooling medium inlet 1d, has the first cooling medium to export 1e above the second heat exchanger tube 1f, and 1 top of the first fluidized bed is equipped with first
Gas vent 1c.The structure of second fluidized bed 2 is identical as the first fluidized bed 1.
As shown in Figure 1, first by two fluidized bed bakers to reaction temperature before driving, then the first raw material reaction gas 5b is from the
First primary air inlet 1a of one fluidized bed 1 enters inside reactor, and the second raw material reaction gas 5a points are two-way respectively from first-class
The second extra-air inlet 2b of the first extra-air inlet 1b and second fluidized bed (2) that change bed 1 enter inside reactor, the first fluidized bed
1 product gas exports 1c from first gas, and the second primary air inlet 2a of second fluidized bed 2 is entered after cooling down by heat exchanger 3, the
The product gas of two fluidized beds 2 goes out battery limit (BL) from second gas outlet 2c discharge, by the cooling heel row of the second heat exchanger 4.First is low
Warm cooling medium 6a divides two-way second cold respectively from the first cooling medium inlet 1d of the first fluidized bed 1 and second fluidized bed 2
But medium entrance 2d enters corresponding first and second heat exchanger tubes 1f, 2f, and the High-temperature cooling medium 7a after heating is from first-class
Change the first cooling medium outlet 1d of bed 1 and the second cooling medium outlet 2d outflow of second fluidized bed 2.Second sub-cooled is situated between
Matter 6b divides two-way to respectively enter First Heat Exchanger 3 and the second heat exchanger 4, and the second High-temperature cooling medium 7b after heating flows out boundary
Area.Catalyst for Oxidative Coupling of Methane reaction is strongly exothermic process, removes waste heat by circulating cooling medium, guarantees that reaction exists
It is carried out under optimal reaction condition.
Using fluidized-bed reactor shown in FIG. 1, use average grain diameter for 80 μm of catalyst granules, the first fluidized bed 1
The first primary air inlet 1a enter reaction gas methane, the second of the first extra-air inlet 1b of the first fluidized bed 1 and second fluidized bed 2
Extra-air inlet 2b enters oxygen and nitrogen, is 720 DEG C in reaction temperature, reaction pressure is normal pressure, air speed 2000h-1, alcoxyl ratio
For 3:1, under conditions of oxygen nitrogen ratio is 1:1, methane conversion 42%, the selectivity of ethylene is 58%.
Embodiment 2
Using fluidized-bed reactor shown in FIG. 1, use average grain diameter for 100 μm of catalyst granules, the of the first fluidized bed 1
One primary air inlet 1a enters reaction gas methane, the second of the first extra-air inlet 1b of the first fluidized bed 1 and second fluidized bed 2 it is secondary into
Port 2b enters oxygen and nitrogen, is 700 DEG C, reaction pressure 0.5MPaG, air speed 9000h in reaction temperature-1, alcoxyl ratio
For 3:1, under conditions of oxygen nitrogen ratio is 1:1, methane conversion 45%, the selectivity of ethylene is 56%.
Embodiment 3
Using fluidized-bed reactor shown in FIG. 1, use average grain diameter for 80 μm of catalyst granules, the of the first fluidized bed 1
One primary air inlet 1a enters reaction gas methane and oxygen, and the of the first extra-air inlet 1b of the first fluidized bed 1 and second fluidized bed 2
Two extra-air inlet 2b enter oxygen and nitrogen, are 720 DEG C, reaction pressure 0.2MPaG, air speed 5000h in reaction temperature-1,
Alcoxyl ratio is 3:1, and under conditions of oxygen nitrogen ratio is 1:1, methane conversion 44%, the selectivity of ethylene is 59%.
Embodiment 4
Using fluidized-bed reactor shown in FIG. 1, use average grain diameter for 50 μm of catalyst granules, the of the first fluidized bed 1
One primary air inlet 1a enters reaction gas methane and oxygen, and the of the first extra-air inlet 1b of the first fluidized bed 1 and second fluidized bed 2
Two extra-air inlet 2b enter oxygen and nitrogen, are 700 DEG C, reaction pressure 0.8MPaG, air speed 14000h in reaction temperature-1,
Alcoxyl ratio is 4:1, and under conditions of oxygen nitrogen ratio is 1:1, methane conversion 38%, the selectivity of ethylene is 61%.
Claims (6)
1. a kind of fluidized-bed reactor for taking heat for methane conversion and intensification, it is characterised in that: convert second processed including two methane
The fluidized bed of alkene, one heat exchanger of each fluidized bed gas outlet connection, the first fluidized bed (1) bottom end is equipped with the first primary air inlet
(1a) and the first extra-air inlet (1b), the first primary air inlet (1a) enter the first fluidized bed (1) instead by the first distribution grid (1j)
It answers in chamber, the first extra-air inlet (1b) is entered in the first fluidized bed (1) reaction chamber by the first distributor pipe (1g), the first fluidized bed
(1) reaction cavity outer wall is made of the first refractory material (1h), has the first heat exchanger tube on the first fluidized bed (1) reaction cavity wall
(1f) has the first cooling medium inlet (1d) below the first heat exchanger tube (1f), has above the first heat exchanger tube (1f) first cold
But media outlet (1e), the first fluidized bed (1) top are equipped with first gas outlet (1c), second fluidized bed (2) and first class
Bed (1) structure is identical.
2. a kind of fluidized-bed reactor for taking heat for methane conversion and intensification as described in claim 1, it is characterised in that: described
The first raw material reaction gas (5b) enter the by the first distribution grid (1j) from the first primary air inlet (1a) of the first fluidized bed (1)
In one fluidized bed (1) reaction chamber, the second raw material reaction gas (5a) is divided into two-way, all the way from the first of the first fluidized bed (1) it is secondary into
Port (1b) is entered in the first fluidized bed (1) reaction chamber by the first distributor pipe (1g), all the way from the second of second fluidized bed (2)
Extra-air inlet (2b) is entered in second fluidized bed (2) reaction chamber by the second distributor pipe (2g), the first fluidized bed (1) product gas
(1c) is exported from first gas, second primary air inlet of second fluidized bed (2) is entered after cooling down by First Heat Exchanger (3)
(2a) is then entered in second fluidized bed (2) reaction chamber by the second distribution grid (2j), the product gas of second fluidized bed (2)
From second gas outlet (2c) discharge, by being discharged after the second heat exchanger (4) cooling, the first low-temperature cooling media (6a) divide two-way
Respectively from the second cooling medium of the first low-temperature cooling media import (1d) of the first fluidized bed (1) and second fluidized bed (2) into
Mouthful (2d) enters the first heat exchanger tube (1f) and the second heat exchanger tube (2f), and the first High-temperature cooling medium (7a) after heating is from the
The first cooling medium outlet (1e) of one fluidized bed (1) and the second cooling medium outlet (2e) outflow of second fluidized bed (2), the
Two low-temperature cooling medias (6b) divide two-way respectively enter First Heat Exchanger (3) and the second heat exchanger (4) exchanged heat after become
The outflow of two High-temperature cooling media (7b).
3. a kind of fluidized-bed reactor for taking heat for methane conversion and intensification as claimed in claim 2, it is characterised in that: described
The first distribution grid (1j) and the second distribution grid (2j) be sintered plate or porous plate.
4. a kind of fluidized-bed reactor for taking heat for methane conversion and intensification as claimed in claim 2, it is characterised in that: described
The first distributor pipe (1g) and the second distributor pipe (2g) be sintering tube or antipriming pipe.
5. a kind of as claimed in claim 2 take the fluidized-bed reactor of heat and technique, feature to exist for methane conversion and intensification
In: the height of first distributor pipe (1g) and the second distributor pipe (2g) is cold lower than the first cooling medium outlet (1e) and second
But media outlet (2e).
6. a kind of as claimed in claim 2 take the fluidized-bed reactor of heat and technique, feature to exist for methane conversion and intensification
In: the first raw material reaction gas (5b) is the mixed gas of methane or methane and oxygen；Second raw material reaction gas (5a)
Nitrogen or nitrogen and oxygen mixed gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910331433.8A CN110252216A (en) | 2019-04-24 | 2019-04-24 | A kind of fluidized-bed reactor taking heat for methane conversion and intensification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910331433.8A CN110252216A (en) | 2019-04-24 | 2019-04-24 | A kind of fluidized-bed reactor taking heat for methane conversion and intensification |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110252216A true CN110252216A (en) | 2019-09-20 |
Family
ID=67913771
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910331433.8A Pending CN110252216A (en) | 2019-04-24 | 2019-04-24 | A kind of fluidized-bed reactor taking heat for methane conversion and intensification |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110252216A (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101804314A (en) * | 2010-05-12 | 2010-08-18 | 新奥新能(北京)科技有限公司 | Fluidized bed reactor |
| CN206152780U (en) * | 2016-10-10 | 2017-05-10 | 中石化上海工程有限公司 | Methane coupling system ethylene reactor structure |
| CN106831306A (en) * | 2017-01-05 | 2017-06-13 | 中石化上海工程有限公司 | Catalyst for Oxidative Coupling of Methane reaction process |
| WO2018072141A1 (en) * | 2016-10-19 | 2018-04-26 | 中国科学院大连化学物理研究所 | Fast fluidized-bed reactor, device, and method using oxygen-containing compound for manufacturing propene or c4 hydrocarbon |
| CN108137435A (en) * | 2015-10-15 | 2018-06-08 | 国际壳牌研究有限公司 | The method of methane oxidative coupling |
| CN108530248A (en) * | 2018-05-08 | 2018-09-14 | 中石化炼化工程（集团）股份有限公司 | A kind of reaction unit and method of Catalyst for Oxidative Coupling of Methane |
-
2019
- 2019-04-24 CN CN201910331433.8A patent/CN110252216A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101804314A (en) * | 2010-05-12 | 2010-08-18 | 新奥新能(北京)科技有限公司 | Fluidized bed reactor |
| CN108137435A (en) * | 2015-10-15 | 2018-06-08 | 国际壳牌研究有限公司 | The method of methane oxidative coupling |
| CN206152780U (en) * | 2016-10-10 | 2017-05-10 | 中石化上海工程有限公司 | Methane coupling system ethylene reactor structure |
| WO2018072141A1 (en) * | 2016-10-19 | 2018-04-26 | 中国科学院大连化学物理研究所 | Fast fluidized-bed reactor, device, and method using oxygen-containing compound for manufacturing propene or c4 hydrocarbon |
| CN106831306A (en) * | 2017-01-05 | 2017-06-13 | 中石化上海工程有限公司 | Catalyst for Oxidative Coupling of Methane reaction process |
| CN108530248A (en) * | 2018-05-08 | 2018-09-14 | 中石化炼化工程（集团）股份有限公司 | A kind of reaction unit and method of Catalyst for Oxidative Coupling of Methane |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110227394A (en) | A kind of fluidized-bed reactor for Catalyst for Oxidative Coupling of Methane | |
| CN110078580A (en) | A kind of fluidized bed reaction and method of Catalyst for Oxidative Coupling of Methane | |
| CN102850183B (en) | Methanol synthesis system and method | |
| CN110142009A (en) | A kind of fluidized bed reaction and technique for Catalyst for Oxidative Coupling of Methane | |
| WO2022011871A1 (en) | Micro-interface reaction system and method of coal-to-ethanol | |
| CN201135882Y (en) | Axis radial direction low resistance synthesis reactor | |
| CN204365252U (en) | A kind of large-scale reactor and device thereof | |
| CN101531336B (en) | Small-sized high efficiency self-heating natural gas hydrogen-preparing device | |
| CN202808648U (en) | Methanol synthetic system | |
| CN105255532A (en) | Fluidized bed and fixed bed combined methanation method | |
| CN110252216A (en) | A kind of fluidized-bed reactor taking heat for methane conversion and intensification | |
| CN104341259B (en) | A kind of catalyzing methanation of synthesis gas method and device | |
| CN102070388B (en) | Micro reaction-heat exchange system for preparing ethylene by using biological ethanol | |
| CN109111967B (en) | Methanation system and method for preparing natural gas from coke oven gas | |
| CN219441616U (en) | Integrated synthesizing tower for preparing methanol by carbon dioxide hydrogenation | |
| CN113086947A (en) | Isothermal series adiabatic conversion system of high concentration CO feed gas | |
| CN203648501U (en) | Corrugated plate type uniform-temperature hydrogenation reactor | |
| CN218901792U (en) | Synthesizer for preparing methanol by carbon dioxide hydrogenation | |
| CN2284099Y (en) | Heat insulating casing externally cooling combined reactor | |
| CN214734507U (en) | Hydrogen production device by water-hydrogen solution cracking | |
| CN219003010U (en) | System for synthesizing methanol by carbon dioxide hydrogenation | |
| CN106966848B (en) | Method for producing ethylene by ethanol dehydration | |
| CN102826965B (en) | Process and device for producing dimethyl ether by gas-phase catalytic dehydration of methanol | |
| CN104230616B (en) | Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system | |
| CN214734506U (en) | Integrated high-purity hydrogen production machine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20190920 |
|
| WD01 | Invention patent application deemed withdrawn after publication |